The present disclosure provide processes of separating aromatic isomers; liquid-liquid extraction systems and processes; liquid-liquid extraction solvents; cucurbituril macrocycle selective for the extraction of aromatic isomers; related materials, methods, and systems; and the like. The process of separating aromatic isomers may include contacting an isomers solution including one or more aromatic isomers, with an aqueous solution including a cucurbituril macrocycle, to produce a first aqueous phase and a first organic phase, wherein the cucurbituril macrocycle is selective for the extraction of at least one of said aromatic isomers.

The present disclosure provide processes of separating aromatic isomers; liquid-liquid extraction systems and processes; liquid-liquid extraction solvents; cucurbituril macrocycle selective for the extraction of aromatic isomers; related materials, methods, and systems; and the like. The process of separating aromatic isomers may include contacting an isomers solution including one or more aromatic isomers, with an aqueous solution including a cucurbituril macrocycle, to produce a first aqueous phase and a first organic phase, wherein the cucurbituril macrocycle is selective for the extraction of at least one of said aromatic isomers.

A process for making 2,3,3,3-tetrafluoropropene (HFO-1234yf) includes providing a composition including 2-chloro-1,1,1,2-tetrafluoropropane (HCFC-244bb) to a reactor including a heater surface at a surface temperature greater than about 850° F. (454° C.), and then bringing the composition into contact with the heater surface for a contact time of less than 10 seconds to dehydrochlorinate a portion of the HCFC-244bb to make HFO-1234yf.

A process for making 2,3,3,3-tetrafluoropropene (HFO-1234yf) includes providing a composition including 2-chloro-1,1,1,2-tetrafluoropropane (HCFC-244bb) to a reactor including a heater surface at a surface temperature greater than about 850° F. (454° C.), and then bringing the composition into contact with the heater surface for a contact time of less than 10 seconds to dehydrochlorinate a portion of the HCFC-244bb to make HFO-1234yf.

A method for producing methyl fluoride, comprising the steps of: (1) pyrolyzing a starting compound in a gas phase to thereby obtain a mixed gas containing methyl fluoride and acid fluoride; and (2) rectifying the mixed gas obtained in step (1) to thereby obtain methyl fluoride.

A method for producing methyl fluoride, comprising the steps of: (1) pyrolyzing a starting compound in a gas phase to thereby obtain a mixed gas containing methyl fluoride and acid fluoride; and (2) rectifying the mixed gas obtained in step (1) to thereby obtain methyl fluoride.

The invention provides for a method of regenerating a solid adsorbent, such as a molecular sieve or activated carbon, using stable fluorinated hydrocarbon compounds such as, for example, HFC-245cb (1,1,1,2,2-pentafluoropropane, as a regeneration fluid.

The invention provides for a method of regenerating a solid adsorbent, such as a molecular sieve or activated carbon, using stable fluorinated hydrocarbon compounds such as, for example, HFC-245cb (1,1,1,2,2-pentafluoropropane, as a regeneration fluid.

The invention provides for a method of regenerating a solid adsorbent, such as a molecular sieve or activated carbon, using stable fluorinated hydrocarbon compounds such as, for example, HFC-245cb (1,1,1,2,2-pentafluoropropane, as a regeneration fluid.

To provide a method for safely and stably storing a hydrochlorofluoroolefin filled in a container for storage, transportation, etc. A method for storing a hydrochlorofluoroolefin in a sealed storage container, wherein the hydrochlorofluoroolefin is stored in such a state that a gas phase and a liquid phase coexist in the storage container, and the concentration of air in the gas phase in the storage container at a temperature of 25° C. is kept to be at most 3.0 vol %, and a method for storing a hydrochlorofluoroolefin in a sealed storage container, wherein the hydrochlorofluoroolefin is stored in such a state that a gas phase and a liquid phase coexist in the storage container, and the concentration of oxygen in the gas phase in the storage container at a temperature of 25° C. is kept to be at most 0.6 vol %.